Simultaneous anoxic biological phosphorus and nitrogen removal with energy recovery

ABSTRACT

Methods and systems are provided for treating wastewater to simultaneously remove nitrogen, carbon, and phosphorus, while recovering energy in the form of methane and carbon dioxide. An ammonia-containing stream is directed to a pretreatment tank that produces excess sludge, biogas, and a pretreated stream. The pretreated stream has at least 45% less carbon than the ammonia-containing stream. The pretreated stream is then directed to an anoxic tank, which promotes phosphorus release and fermentation of particulate and dissolved organic matter. The mixed liquor is transferred to an aerated tank having low dissolved oxygen concentrations to promote development of phosphorus-release bacteria that is eventually recycled to the anoxic tank by way of the return activated sludge. Simultaneous nitrification, denitrification, and phosphorus release occur in the aerated tank. A membrane tank separates treated effluent from activated sludge in a membrane tank.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part application of and claimspriority to U.S. application Ser. No. 12/886,321 filed Sep. 20, 2010,entitled “SIMULTANEOUS ANOXIC BIOLOGICAL PHOSPHORUS AND NITROGENREMOVAL,” which is hereby incorporated by reference in its entirety.

BACKGROUND

Removing various components from wastewater, such as nitrogen, carbon,and phosphorus can be a difficult and high-cost process that in someinstances may require the addition of a carbon source to wastewatertreatment process. Additionally, a high concentration of dissolvedoxygen used in many wastewater treatment processes contributessubstantially to the cost of energy usage of a wastewater treatmentplant. A carbon source, such as methanol, may be added to the process inan anoxic tank, for example, to assist with denitrification. Further, anaerated tank may require high concentrations of dissolved oxygen topromote oxidation of biological oxygen demand (BOD) and ammonia. Theaddition of a carbon source and the requirement of high concentrationsof dissolved oxygen, however, are costly and significantly contribute tothe expense of treating wastewater.

SUMMARY

Embodiments of the invention are defined by the claims below, not thissummary. A high-level overview of various aspects of the invention areprovided here for that reason, to provide an overview of the disclosure,and to introduce a selection of concepts that are further described inthe detailed-description section below. This summary is not intended toidentify key features or essential features of the claimed subjectmatter, nor is it intended to be used as an aid in isolation todetermine the scope of the claimed subject matter.

In a first aspect, a process is provided for treating wastewater tosimultaneously remove organic matter, nitrogen, and phosphorus withenergy recovery. The process includes providing an ammonia-containingstream in a pretreatment tank that produces, at least, excess sludge,biogas, and a pretreated stream. The pretreated stream has at least 45%less carbon than the ammonia-containing stream. Further, the biogascomprises at least methane and carbon dioxide. The process additionallyincludes flowing the pretreated stream and return activated sludge to ananoxic tank operating under anoxic conditions and mixing the pretreatedstream and the return activated sludge in the anoxic tank to form amixed liquor, thereby initiating phosphorus release and fermentation ofparticulate organic matter and dissolved organic matter. Further, theprocess includes transferring the mixed liquor to an aerated tankoperating under microaerophilic conditions. A concentration of dissolvedoxygen in the aerated tank is less than 1.0 mg/l of the mixed liquor,which is effective to promote simultaneous nitrification,denitrification, phosphorous release, and phosphorus uptake. Also, theprocess includes transferring the mixed liquor to a membrane tank thatseparates treated effluent from activated sludge containingmicroorganisms. A first portion of the activated sludge is returned tothe anoxic tank as the return activated sludge.

In a second aspect, a method is provided for reducing ammonia in astream while recovering energy. The method includes providing a streamcontaining ammonia in a pretreatment tank that comprises anaerobicmicroorganisms that reacts with the ammonia-containing stream to producebiogas and a pretreated stream. Further, the method includes contactingthe pretreated stream with an oxygen-containing stream under effectivetreatment conditions to form a first product stream, the ratio ofammonia in the pretreated stream to oxygen in the oxygen-containingstream being about 2.28 g O2/g N—NH3 (2.28 grams of oxygen per gram ofnitrogen in ammonia) or less. The method additionally includes exposingthe first product stream to organic matter under effective treatmentconditions in a ratio of about 0.57 g COD/g N—NH3 (0.57 grams ofchemical oxygen demand (COD) per gram of nitrogen in ammonia) or les.

In a third aspect, a system for treating wastewater to simultaneouslyremove organic matter, nitrogen, and phosphorus with energy recovery isprovided. The system includes a pretreatment tank that receives plantinfluent wastewater and that comprises anaerobic microorganisms thatreacts with the plant influent wastewater to produce, at least, biogascomprising methane, excess sludge, and a pretreated stream, thepretreated stream having at least 45% less carbon than the plantinfluent wastewater. The system also includes an anoxic tank thatreceives the pretreated stream and return activated sludge. The anoxictank operates under anoxic conditions to promote denitrification,phosphorus release and fermentation of particulate organic matter anddissolved organic matter. Further, the system includes an aerated tankthat receives a mixed liquor from the anoxic tank. A concentration ofdissolved oxygen in the aerated tank is less than 1.0 mg/l of the mixedliquor to effectively promote development of phosphorus-release bacteriathat is present in the return activated sludge received into the anoxictank. The phosphorus-release bacteria in the return activated sludgeallows for the phosphorus release and fermentation of particulateorganic matter in the anoxic tank. The system additionally includes amembrane tank that separates plant effluent wastewater from activatedsludge, a portion of which is recycled to the anoxic tank as the returnactivated sludge.

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

Illustrative embodiments of the present invention are described indetail below with reference to the attached drawing figures, andwherein:

FIG. 1 illustrates a schematic view of a wastewater treatment process,in accordance with an embodiment of the present invention;

FIG. 2 illustrates a schematic view of an alternate wastewater treatmentprocess, in accordance with an embodiment of the present invention;

FIG. 3 illustrates a decrease of energy usage at a wastewater treatmentplant as a result of implementation of embodiments of the presentinvention;

FIG. 4 illustrates a decrease of both ammonia and phosphate whenembodiments of the present invention are implemented in a wastewatertreatment plant;

FIG. 5 illustrates a bar graph showing the concentrations of phosphorus,dissolved oxygen, and nitrates in each tank;

FIG. 6 illustrates a schematic view of a wastewater treatment processwith energy recovery, in accordance with an embodiment of the presentinvention;

FIG. 7 illustrates a schematic view of a wastewater treatment processthat utilizes an upflow anaerobic sludge blanket (UASB) reactor, inaccordance with an embodiment of the present invention;

FIG. 8 illustrates a schematic view of a wastewater treatment processthat utilizes chemically enhanced primary treatment (CEPT), inaccordance with an embodiment of the present invention;

FIG. 9 illustrates a schematic view of a wastewater treatment processthat utilizes a one-stage activated sludge system, in accordance with anembodiment of the present invention;

FIG. 10 illustrates a schematic view of a wastewater treatment processthat utilizes a one-stage activated sludge system, in accordance with anembodiment of the present invention;

FIG. 11 illustrates a bar graph showing a comparison of energy intensityusing various water treatment systems, in accordance with an embodimentof the present invention; and

FIG. 12 illustrates a bar graph showing a comparison of energygeneration from biogas, in accordance with an embodiment of the presentinvention.

DETAILED DESCRIPTION

The subject matter of embodiments of the present invention is describedwith specificity herein to meet statutory requirements. But thedescription itself is not intended to necessarily limit the scope ofclaims. Rather, the claimed subject matter might be embodied in otherways to include different steps or combinations of steps similar to theones described in this document, in conjunction with other present orfuture technologies. Terms should not be interpreted as implying anyparticular order among or between various steps herein disclosed unlessand except when the order of individual steps is explicitly described.

FIG. 1 illustrates a schematic view of a wastewater treatment process10. More specifically, the wastewater treatment process provides anenergy and cost efficient method for the simultaneous removal ofnitrogen, phosphorus, and organic matter from plant influent wastewater.While many systems require an external carbon source and high levels ofdissolved oxygen, embodiments of the present invention do not requireeither, and in fact require very low amounts of dissolved oxygen andcarbon in comparison to amounts typically used in wastewater treatmentsystems. For instance, many systems require an external carbon sourcefor phosphorus removal and nitrogen removal, but in embodiments of thepresent invention, nitrogen removal requires only minimum amounts ofcarbon, as it uses mostly ammonia. Further, phosphorus removal usesdissolved and particulate carbon (e.g., particulate organic matter) thatis present in the wastewater, instead of only dissolved carbon or anexternal carbon source. In the embodiment of FIG. 1, three separatetanks are used to simultaneously remove nitrogen, phosphorus, andorganic matter from plant influent wastewater 12. As used herein, plantinfluent wastewater 12 is raw wastewater that has not yet been treatedand therefore has not yet entered a wastewater treatment system, such asthe wastewater treatment systems that are described herein.

A first tank shown in FIG. 1 is an anoxic tank 16 that receives at leasttwo streams, including the plant influent wastewater 12 and returnactivated sludge 14. As will be discussed further herein, the returnactivated sludge 14 is a portion of activated sludge that is recycledfrom the third tank, or the membrane tank 20, into one or more of theother tanks, such as the anoxic tank 16. As used herein, activatedsludge is a stream that has been separated from the plant effluent. Thisactivated sludge stream contains a microbial mass, in addition tonitrates and dissolved oxygen. The microbial mass includes a variety ofbiological components, including bacteria, fungi, protozoa, rotifers,etc. While both heterotrophic and autotrophic microorganisms may residein activated sludge, heterotrophic microorganisms typically predominate.Heterotrophic microorganisms obtain energy from carbonaceous organicmatter in plant influent wastewater for the synthesis of new cells.These microorganisms then release energy via the conversion of organicmatter into compounds, such as carbon dioxide and water. Autotrophicmicroorganisms in activated sludge generally reduce oxidized carboncompounds, such as carbon dioxide, for cell growth. These microorganismsobtain their energy by oxidizing ammonia to nitrate, known asnitrification, which is further described herein.

As mentioned above, the return activated sludge 14 is a portion of theactivated sludge that is produced by the separation step (e.g., membranetank or membrane bioreactor) at the end of the treatment process. Thereturn activated sludge 14 is recycled into the anoxic tank 16 andprovides the tank with microbial mass, residual oxygen, nitrates, andnitrites. It should be noted that phosphorus release typically does notoccur in anoxic tanks with return activated sludge having nitrates anddissolved oxygen, but in embodiments of the present invention,phosphorus release does occur in the anoxic tank 16. Phosphorus releaseoccurs because the bacteria that is used to consume phosphorus is alsopresent in the return activated sludge 14. Additionally, phosphorusrelease occurs because of active hydrolysis and fermentation conditionsof particulate organic matter present in the influent wastewater. Asused herein, hydrolysis is the breakdown of polymeric organic matterinto monomers by microbial action. In one embodiment, hydrolysis refersto a chemical reaction during which molecules of water are split intohydrogen cations and hydroxide anions in the process of a chemicalmechanism. This type of reaction is used to break down certain polymers.As such, instead of just using dissolved organic matter as the carbonsource for phosphorus removal, embodiments of the present inventionallow for both dissolved and particulate organic matter to be used as acarbon source for phosphorus removal. Normally particulate organicmatter cannot be used, but because it is fermented here, it can be usedas a carbon source, thus eliminating the need for an external carbonsource.

In wastewater, organic matter occurs as particulate organic matter anddissolved organic matter. Three main tests are used for determining theorganic matter in wastewater. These include biological oxygen demand(BOD), total organic carbon (TOC), and chemical oxygen demand (COD).Unlike dissolved organic matter, particulate organic matter takes theform of suspended solids found in wastewater. As further discussedherein, particulate organic matter undergoes the process of hydrolysisto convert the particulates into soluble solids, thus allowing forhigher rates of phosphorus removal when embodiments of the presentinvention are utilized.

Phosphorus release and phosphorus uptake refer to the process ofphosphorus accumulating organisms (PAOs) storing polyphosphate as anenergy reserve in intracellular granules. In anaerobic conditions, thePAOs release orthophosphate, utilizing the energy to accumulate simpleorganics and store them as polyhydroxyalkanoates (PHAs). In aerobicconditions, or at least conditions where there is some oxygen, nitrites,or nitrates present, the PAOs grow on the stored organic material, usingsome of the energy to take up orthophosphate and store it aspolyphosphate. As such, when the PAOs store carbon for future growth,the PAOs also release phosphorus, sometimes simultaneously. When thePAOs use stored carbon, they uptake phosphorus using preferentiallynitrite as an electron acceptor. As will be further described herein, anaerated tank has low levels of dissolved oxygen, but the PAOs stilluptake phosphorus. When oxygen, nitrite, or nitrate is present, the PAOscan get energy out of the carbon. Therefore when carbon is abundant, thePAOs store it in their cells and wait until there are conditions wherean electron acceptor is present so that they can use the carbon forgrowth and uptake phosphorus. The phosphate is then removed in the wasteactivated sludge 26, which is generally the activated sludge that is notrecycled to the anoxic tank 16. The development of the PAO populationwill be discussed further herein. The anoxic tank 16 operates underanoxic conditions such that there is little to no dissolved oxygen, butnitrates (e.g., NO2 and NO3) may be present. A continuous oxygen deficitis maintained in the anoxic tank.

The anoxic tank 16, in one embodiment, has a mixer that mixes the plantinfluent wastewater 12 and the return activated sludge 14 to form amixed liquor. The mixed liquor, as used herein, simply refers to amixture of plant influent wastewater 12 and return activated sludge 14.The rate of mixing may be adjusted, in addition to adjusting the flowrate of the return activated sludge 14, to control the phosphorusrelease in the anoxic tank 16. It should be noted that the addition ofan external carbon source, such as methanol, is avoided in embodimentsof the present invention such that there is no additional carbon sourceneeded to carry out embodiments of the present invention. In addition tophosphorus release, denitrification also occurs in the anoxic tank 16.Denitrification is the breakdown of nitrites or nitrates to give offnitrogen gas, and occurs as microbes consume oxygen from the nitrites ornitrates. More specifically, denitrification is a microbiallyfacilitated process of dissimilatory nitrate reduction ultimatelyproducing molecular nitrogen (N2), which is returned to the atmosphere.Nitrates and nitrites are converted into nitrogen gas by way of adenitrification process. Denitrification generally reduces oxidizedforms of nitrogen in response to the oxidation of an electron donor,such as organic matter which, here, is present in the return activatedsludge 14. This process is performed primarily by heterotrophicmicroorganisms in an environment where oxygen is depleted, or whereoxygen consumption exceeds the rate of oxygen supply, such as the anoxictank 16 and the aerated tank 18. Utilizing embodiments of the presentinvention, the denitrification process is also conducted by autotrophicnitrifiers under conditions of low dissolved oxygen in the anoxic tank16 and the aerated tank 18. The following reactions illustrate thedenitrification process, including an illustrative redox reaction:NO₃ ⁻→NO₂ ⁻→NO+N₂O→N₂(g)  (1)2NO₃ ⁻+10e ⁻+12H⁺→N₂+6H₂O  (2)

Particulate organic matter and dissolved organic matter from the plantinfluent wastewater 12 are fermented in the anoxic tank. The conditionsin the anoxic tank in embodiments of the present invention induce highrates of hydrolysis and fermentation of particulate organic matter,which provides fermented organic matter in excess of what is needed forthe denitrification reaction, allowing for simultaneous release ofphosphorus and the formation of PHAs. The fermentation of particulateorganic matter allows for additional carbon to be used for phosphorusremoval. The average detention time of the influent wastewater flow inthe anoxic tank may vary from one hour to ten hours. In one embodiment,the dissolved oxygen concentration in the anoxic tank is less than 0.3mg/L. In further embodiments, the dissolved oxygen concentration in theanoxic tank is less than 0.2 mg/L. In an even further embodiment, thedissolved oxygen concentration in the anoxic tank is 0.1 mg/L or less.Further, recirculation rates of the return activated sludge may varybetween 0.3 to 6 times the influent flow rate.

The anoxic mixed liquor is transferred to an aerated tank 18. While asingle aerated tank 18 is illustrated in FIG. 1, multiple aerated tanksmay be used, and may be configured either in parallel or in series.Alternatively, one aerated tank may be used, but the aerated tank mayhave more than one compartment through which the mixed liquor flows. Thepurpose of having more than one compartment is to improve the kineticconditions of the overall process minimizing tank volume. Optionally, aportion of the activated sludge is transferred into the aerated tank toprovide an additional microbial population needed to ferment theparticulate and dissolved organic matter and to promote phosphorusrelease. This is advantageous in those cases where the nitrateconcentrations in the membrane tank are excessively high. Unlike manyaerated tanks, the aerated tank 18 provided for in embodiments of thepresent invention is operated under very low dissolved oxygenconcentrations, such as microaerophilic conditions, which promotes thedevelopment of the microbial population (e.g., phosphate accumulatingorganisms (PAO)) used for phosphorus release and uptake. Generally, thisbacterial population is capable of storing phosphorus, such as in theform of polyphosphates, and metabolizes it for energy production andcell synthesis, resulting in the removal of phosphorus from the systemthrough the activated sludge. This particular microbial population isunable to develop where there are high concentrations of dissolvedoxygen. Since this particular bacterial population is able to develop inthe aerated tank 18, it is also present in the return activated sludge14 that is recycled to the anoxic tank 16, thereby allowing forphosphorus release in the anoxic tank 16. Phosphorus uptake may occursimultaneously with phosphorus release in the aerated tank 18.

In addition to phosphorus release and phosphorus uptake, nitrificationand denitrification also occur in the aerated tank 18. In oneembodiment, nitrification, denitrification, and phosphorus release occursimultaneously in the aerated tank 18. As previously described,denitrification is a microbially facilitated process of dissimilatorynitrate reduction that ultimately produces nitrogen gas by reducingoxidized forms of nitrogen. Nitrification, on the other hand, is thebreakdown of ammonia into nitrate and water. More particularly,nitrification is the biological oxidation of ammonia with oxygen intonitrite followed by the oxidation of nitrites into nitrates. Two groupsof organisms are generally responsible for the oxidation of ammonia intonitrite. These two groups are ammonia-oxidizing bacteria (AOB) andammonia-oxidizing archaea (AOA). A second group is nitrite oxidizingbacteria, NOB, is responsible for oxidation of nitrites to nitrates. Thefollowing equations represent the nitrification process:NH₃+CO₂+1.5O₂+AOA/AOB→NO₂ ⁻+H₂O+H⁺  (3)NO₂ ⁻+CO₂+0.5O₂+NOB→NO₃ ⁻  (4)NH₃+O₂→NO₂ ⁻+3H⁺+2e ⁻  (5)NO₂ ⁻+H₂O→NO₃ ⁻+2H⁺+2e ⁻  (6)

In embodiments of the present invention, however, the reactionsrepresented by equations (4) and (6) occur at a minimum, thus reducingthe need for oxygen and obtaining significant savings in energy usage.In some embodiments, very little to no nitrates are found in the mixedliquor because reactions (4) and (6) are such a small percentage of theoverall process such that in equation (1) above, it is mainly nitritesrather than nitrates being converted to nitrogen gas. As such, inequation (2), there are less than 10 electrons needed to convert nitriteto nitrogen gas. In embodiments of the present invention, theseelectrons, rather than coming from methanol or another external carbonsource, come from ammonia. In embodiments of the present invention, PAObacteria can also use nitrites as electron acceptors fordenitrification. This will be discussed in more detail below. As shownby reactions (3) and (5) above, ammonia is used to convert nitrites intonitrogen gas. As an external carbon source is not required, some of theammonia is used for reactions (3) and (5), but some of the ammonia isalso used as a reducing source of electrons for denitrification. This ishow nitrification and denitrification can occur in systems with lowoxygen concentrations and without an external carbon source.

Further, the microaerophilic conditions allow for fermentation ofparticulate and dissolved organic matter in the aerated tank 18, whichwould not typically occur with higher concentrations of dissolvedoxygen.

As mentioned above, nitrification and denitrification occur in both theanoxic and aerated tanks, according to embodiments of the presentinvention. Conventional nitrification-denitrification is represented byreactions (7), (8), and (9) below. Reaction (9) is the net of reactions(7) and (8). Many times, this sequence of reactions requires a highconcentration of dissolved oxygen and an external carbon source. Here,about 4.57 grams of O2 per gram of N—NH3 are required for reaction (7)and about 2.86 grams of COD-O2 per gram of N—NO3 are required forreaction (8). The equations are as follows:

$\begin{matrix}\left. {{1\;{NH}_{3}} + {2\; O_{2}}}\rightarrow{{1\;{HNO}_{3}} + {H_{2}O}} \right. & (7) \\\left. {{1\;{HNO}_{3}} + {{Organic}\mspace{14mu}{Matter}}}\rightarrow{{\frac{1}{2}N_{2}} + {H_{2}O}} \right. & (8)\end{matrix}$

Reactions (9) and (10) below illustrate a process called a nitrificationshortcut where the initial reaction, or reaction (10), is driven only tonitrite, which results in a savings in the needs of both oxygen demandand organic matter. About 3.43 grams of O2 per gram of N—NH3 is requiredfor reaction (9) and about 1.71 grams of COD-O2 per gram of N—NH3 arerequired for reaction (10). In one instance, when comparing the firstset of reactions above (reactions (7)-(8)) to the second set ofreactions below (reactions (9)-(10)), the oxygen demand is decreased byabout 25% (4.57 g O2/g N—NH3−3.43 g O2/g N—NH3=1.15 g O2/g N—NH3) andthe need for organic matter is decreased by about 40% (2.86 g O2/gN—NO3−1.71 g O2/g N—NH3=1.15 g COD/g N—NH3). This set of reactionsoccurs in the anoxic tank and the aerated tank with PAO bacteria, whichpreferentially catalyze reaction (10) below.

$\begin{matrix}\left. {{1\;{NH}_{3}} + {\frac{3}{2}\; O_{2}}}\rightarrow{{1\;{HNO}_{2}} + {1H_{2}O}} \right. & (9) \\\left. {{1\;{HNO}_{2}} + {{Organic}\mspace{14mu}{Matter}}}\rightarrow{{\frac{1}{2}N_{2}} + {H_{2}O}} \right. & (10)\end{matrix}$

The set of reactions below labeled (11) and (12) occur in the anoxictank and the aerated tank. In some instances, this set of reactions isreferred to as a nitrifier-denitrification process. As shown in equation(11), ammonia and oxygen are converted into nitrogen gas, nitrous acid,and water. Organic matter is then used to convert the nitrous acid intonitrogen gas, water, and carbon dioxide. About 2.28 grams of O2 per gramof N—NH3 is required for reaction (11) and about 0.57 grams of COD pergram of N—NH3 is required for reaction (12). When comparing the threesets of reactions, this third set of reactions (reactions (13)-(15))requires the least amount of oxygen. The savings in organic matter isabout 80% (2.86 g O2/g N—NO3−0.57 g COD/g N—NH3=2.29 g O2/g N) whencomparing the amount of organic matter required for the third set ofreactions below to the first set of reactions (reactions (7)-(8)).Further, the savings in oxygen required between the first and the thirdset of equations is about 50% (4.57 g O2/g N—NH3−2.28 g O2/g N—NH3=2.28g O2/g N).

$\begin{matrix}\left. {{1\;{NH}_{3}} + {1O_{2}}}\rightarrow{{\frac{1}{3}N_{2}} + {\frac{1}{3}\;{HNO}_{2}} + {\frac{4}{3}H_{2}O}} \right. & (11) \\{\;\left. {{\frac{1}{3}{HNO}_{2}} + {{Organic}\mspace{14mu}{Matter}}}\rightarrow{{\frac{1}{6}N_{2}} + {H_{2}O} + {CO}_{2}} \right.} & (12)\end{matrix}$

Returning to FIG. 1, the mixed liquor is then transferred from theaerated tank 18 to a third tank, here shown as a membrane tank 20, for asolid-liquid separation step where the microorganisms are separated fromthe treated water. In activated sludge processes, such as thosedescribed herein, the dissolved organic pollutants are transformed intowater, carbon dioxide, and biomass, which results in an excessproduction of sludge. The membrane tank 20 separates this sludge fromthe treated plant effluent 22. In one embodiment, the membrane tank is amembrane bioreactor that is a combination of a membrane process (e.g.,microfiltration, ultrafiltration, hollow fiber, flat sheet, tubular)with a suspended growth bioreactor. A bioreactor refers to a device thatsupports a biologically active environment. Because a bioreactor must beassociated with a separation unit to recover the biomass and thepurified liquid, and of the inefficiencies and inconvenience of separateunits, membrane bioreactors are used to provide the same or betterresults, but in a single unit. As such, a membrane bioreactor is anassociation of a biologic reactor and a cross-flow filtration. In oneinstance, the membrane tank 20 is aerated to provide water turbulencefor scouring the submerged membrane filter. In one embodiment, themembrane filter utilized microfiltration, but in another embodiment,ultrafiltration is used.

The result of the membrane filtration occurring in the membrane tank 20is at least two exit streams, including treated plant effluent 22 andactivated sludge 24, a portion of which is recycled to the anoxic tank16, and in some embodiments, to the aerated tank 18. As used herein,treated plant effluent 22 is the stream exiting the third tank that hasbeen treated for the removal of carbon, nitrogen, phosphorus, and otherunwanted constituents. The excess activated sludge is shown as activatedsludge 26. The amount of activated sludge 24 that is recycled to theanoxic tank 16 varies, but in some embodiments ranges anywhere from 50%to 600% of the amount of plant influent wastewater 12 entering theanoxic tank 16. As such, for every one gallon of plant influentwastewater 12, 0.5 to 6 gallons of return activated sludge 14 may beadded to the anoxic tank 16. In an alternative embodiment, the thirdtank in the embodiment of FIG. 1, although illustrated as a membranetank 20, is a clarifier. Clarifiers are tanks used to separate, thicken,and recycle the activated sludge. Typically, clarifiers have a muchlarger footprint than membrane bioreactors.

Referring now to FIG. 2, a schematic view is illustrated of an alternatewastewater treatment process. An anoxic tank 16 a, an aerated tank 18 a,and a membrane tank 20 a are illustrated in the embodiment of FIG. 2 andoperate similarly to those described in FIG. 1. Here, an anaerobic tank28 is added downstream of, or after the anoxic tank 16 a and upstreamof, or before the aerated tank 18 a. Generally, the anaerobic tank 28operates under anaerobic conditions, or under the absence of oxygen. Theanaerobic tank 28 is a non-aerated tank, such that there is no addedoxygen and there are no nitrates. The contents are mixed in theanaerobic tank 28 such that a mixer is present. The embodiment of FIG.2, or specifically where an anaerobic tank 28 is added to the system, isused in conditions where the characteristics of the organic matterpresent in the influent wastewater stream are such that additionalretention time is needed for both hydrolysis and fermentation of theparticulate organic matter. In one embodiment, additional phosphorusrelease takes place in the anaerobic tank 28. Similar to that describedin FIG. 1, plant influent wastewater 12 a is mixed with return activatedsludge 14 a in an anoxic tank 16 a. The mixed liquor is firsttransferred to an anaerobic tank 28, then to an aerated tank 18 a, andfinally to a membrane tank 20 a. Exiting from the membrane tank 20 a istreated plant effluent 22 a and activated sludge 24 a. A portion of theactivated sludge 24 a is recycled to the anoxic tank 16 a as returnactivated sludge 14 a, and optionally, a portion is also recycled to theaerated tank 18 a. The waste activated sludge 26 a, in one embodiment,is disposed of.

FIG. 3 illustrates a line graph 300 showing a decrease of energy usageat a wastewater treatment plant as a result of the implementation ofembodiments of the present invention. As mentioned, when dissolvedoxygen concentrations are kept to a minimum in the aerated tank, energyusage costs significantly decrease, as the addition of dissolved oxygencosts may account for up to 50% of total energy costs for a wastewatertreatment plant. As indicated by “trial started,” the technologydescribed herein was tested and it was found that energy costssignificantly decreased at least partially due to the low amounts ofdissolved oxygen required in the aerated tank. As shown, before thetrial, the highest energy usage is about 64,000 kWh/month, while thehighest after the trial is about 54,000 kWh/month, although the levelsreached much lower amounts for previous months.

Turning now to FIG. 4, a bar graph 400 is illustrated that shows adecrease of both ammonia and phosphate when embodiments of the presentinvention are implemented in a wastewater treatment plant. As shownhere, influent concentrations of ammonia were around 72 mg/l, butdropped to around 1 mg/l after the plant influent wastewater was treatedusing the treatment methods described herein. Further, influentconcentrations of phosphate dropped from around 74 mg/l to around 4 mg/lafter the plant influent wastewater was treated using the treatmentmethods described herein.

EXAMPLE

The following example illustrates a plant that has two parallel trains,including a first train (train A) and a second train (train B). Thetanks in each trains are identical and are in the same location. Theconditions in the tanks, however, are different. Train A represents atypical process that would occur without the user of embodiments of thepresent invention, while train B represents a process that usesembodiments of the present invention, such as a low dissolved oxygenconcentration in the aerated tank, as previously discussed. For example,as shown below in Table 1, the dissolved oxygen concentration in theaerated tank of train A is 1.3 mg/l, while the dissolved oxygenconcentration in the aerated tank of train B is 0.1 mg/l. As shown bythe levels of phosphorus and nitrate/nitrite removal, in train Bcompared with those of train A, the lower levels of dissolved oxygen inthe aerated tank allow for the development of the phosphorus-removalbacteria in the aerated tank. These phosphorus-removal bacteria are thenpresent in the return activated sludge (not shown) from the membranetank back to the anoxic tank. Phosphorus release is observed in theanoxic tank of train B, while not in the anoxic tank of train A. Netphosphorus uptake takes place in the aerated tank of train B and not inthe aerated tank of train A. Therefore, higher levels of phosphorusuptake and removal in the process occur. As a result, the levels ofphosphorus in the membrane tank or the plant effluent are 3.65 mg/l fortrain B, which is much lower than the levels in the membrane tank fortrain A, which are 7.41 mg/l. Similarly, simultaneousnitrification-denitrification take place in the aerated tank of train Bwhile only nitrification takes place in the aerated tank of train A, asreflected by the significantly higher difference in nitrateconcentration. The levels of nitrates/nitrites in the membrane tank fortrain B are 7.15 mg/l, which is lower than the 8.31 mg/l levels in themembrane tank of train A.

Continuing with the example described above and illustrated in Table 1below, FIG. 5 illustrates a bar graph 500 showing the concentrations ofphosphorus, dissolved oxygen, and nitrates in each tank. In comparingthe levels of phosphorus, for example, it can be seen that the levelsare much lower in the membrane tank for train B than for train A, whichis due, in part, to the low dissolved oxygen concentrations in theaerated tank.

TABLE 1 Concentrations of dissolved oxygen, phosphorus, and nitrates ina typical process (Train A) and processes using embodiments of thepresent invention (Train B).

Turning now to FIG. 6, a schematic view 600 of a wastewater treatmentprocess with energy recovery is illustrated, in accordance with anembodiment of the present invention. Embodiments of the presentinvention described herein are referred to in FIG. 6 as the Anox-Pprocess 620. The Anox-P process 620, in embodiments, refers to systemssuch as that depicted in FIG. 1 that includes an anoxic tank, at leastone aerated tank, and a membrane tank. However, in the embodiment ofFIG. 6 prior to the Anox-P process 620, a carbon-removal pretreatmentprocess 612 is added to the overall process. The functionality of thecarbon-removal pretreatment process 612 is to remove a substantialamount of the carbon from the incoming plant influent wastewater 610.Generally, soluble organic matter and particulate organic matter areconverted into an insoluble gas, herein referred to as biogas 614.Because the Anox-P process 620 as described herein requires less carbonthan other systems, the amount of carbon present in the plant influentwastewater 610 may be greater than what is actually needed. Otherwastewater systems require much more carbon (e.g., to remove nitrogen)such that using a carbon-removal pretreatment process 612 would not evenbe considered because the carbon in the plant influent wastewater 610,in addition to carbon in excess of what is in the plant influentwastewater 610, would be required for treating the wastewater. Byremoving so much carbon from the influent stream in the pretreatmentprocess, less oxygen is used in the aerated tank to remove carbon. Assuch, the main advantages of the system as shown in FIG. 6 is thatmethane is produced, and that less air or oxygen is required in theAnox-P process 620. Additionally, the size of the tanks required for theAnox-P process 620 may decrease as compared to the Anox-P process whencarbon is not removed by a pretreatment process.

The carbon-removal pretreatment process 612 may utilize varioustechnologies that are capable of removing a substantial amount of carbonfrom an influent stream. A few of these technologies are listed anddescribed herein for exemplary purposes only, and are not meant to limitembodiments of the present invention. For instance, some of thesecarbon-removing technologies may include an anaerobic process, such asan upflow anaerobic sludge blanket (UASB) reactor, a chemically enhancedprimary treatment (CEPT), and a one-stage activated sludge system(sometimes referred to as the “A” in the A/B process). Again, thesetechnologies are listed for exemplary purposes only, as there are otheravailable technologies not listed herein for the sake of brevity. Moredetails on each of these exemplary technologies are discussed hereinwith respect to subsequent figures.

In embodiments, the carbon that is removed from the plant influentwastewater 610 takes the form of methane (CH4) and/or carbon dioxide(CO2). In one embodiment, a biogas 614 comprising methane and carbondioxide if formed. The biogas 614, once formed, is directed to otherprocesses that are not described herein, but collectively referred to asbiogas utilization 616. This biogas 614, for example, may be used forenergy in fuel cells, microturbines, generators, etc. to generateelectric power to offset part or all of the electric power used at thewater treatment plant. Here, the carbon dioxide may be removed prior tobeing used in these systems. Alternatively, the biogas 614 may betreated (e.g., removal of carbon dioxide) and upgraded, such as byremoving the majority of the carbon dioxide to produce natural gas,which can be used in a compressed form to produce compressed naturalgas, CNG, or alternatively can be liquefied to produce liquefied naturalgas, LNG. In one instance, about 60% of the carbon present in the plantinfluent wastewater 610 is removed by way of the processes and reactionsthat occur in the carbon-removal pretreatment process 612 such thatabout 40% of the carbon is left in the pretreated stream 618. In anotherinstance, about 70% of the carbon present in the plant influentwastewater 610 is removed by way of the processes and reactions thatoccur in the carbon-removal pretreatment process 612 such that about 30%of the carbon is left in the pretreated stream 618. In yet anotherinstance, less than 60% of the carbon, such as 45% of the carbon isremoved from influent stream by way of the carbon-removal pretreatmentprocess 612. The biogas 614 itself, in one embodiment, is comprised ofup to 80% methane. The other portion of the biogas 614 may be a mixtureof carbon dioxide, nitrogen, and hydrogen sulfide in differentproportions. The proportion of methane to the other portion may varysignificantly depending on operational conditions of the wastewatertreatment plant, and thus the examples provided herein are for exemplarypurposes only and are not meant to limit embodiments of the presentinvention. For instance, the percentage of methane in one embodiment maybe 50%, but in an alternate embodiment may be 80%. As mentioned,compared to traditional wastewater treatment systems, much less carbonis required using the embodiments described herein to convert nitrogenin the ammonia to nitrogen gas, water, and carbon dioxide. As such, itis feasible to remove a large percentage of the carbon from the plantinfluent wastewater, such that enough carbon is still available in theAnox-P process to convert nitrogen to the products listed above. Usingother systems that similarly treat wastewater, it would not be possibleto remove this amount of carbon, or any carbon at all, as these systemstypically require the addition of carbon, in addition to the carbonpresent in the wastewater. Combining the carbon removal pretreatment andAnox-P process enables a high-efficiency process that removes carbon,nitrogen, phosphorus, and fermentation of particulate and dissolvedorganic matter from wastewater without the need for external sources ofcarbon and recovering energy in the form of biogas.

In one embodiment, conditions in the carbon-removal pretreatment process612 include a temperature of 18° C. or higher. When temperatures areless than this, the same results can be obtained but with efficienciesthat are slightly lower, such as a carbon removal of around 40-60%,instead of closer to 70%. In one instance, a portion of the plantinfluent wastewater 610 is diverted prior to entering the carbon-removalpretreatment process 612 and is mixed in with the pretreated stream 618.This may occur when there is a high ammonia concentration, or highamounts of nitrogen in this stream, such as is the case with raw sewagewith the food industry wastewater components or some water reuseapplications. Some of the incoming stream may be bypassed so that thereis more carbon in the pretreated stream 618 before it enters the Anox-Pprocess 620. When ammonia or nitrogen levels in general are high, morecarbon is needed to remove the nitrogen in the Anox-P process 620.

FIG. 7 illustrates a schematic view 700 of a wastewater treatmentprocess that utilizes an upflow anaerobic sludge blanket (UASB) reactor,in accordance with an embodiment of the present invention. Generally, aUASB reactor is a methanogenic digester that produces, at least,methane. A UASB reactor is a form of an anaerobic digester that is used,typically, in the treatment of wastewater. An anaerobic process is usedby the UASB reactor wherein a blanket of granular sludge is formed thatis suspended in the tank. Generally, wastewater flows upwards throughthe sludge blanked such that the wastewater is treated by anaerobicmicroorganisms. In some cases, flocculants are used to aid thesuspension of the sludge blanket. A by-product comprising methane,typically in high concentrations, is produced. As mentioned, the biogasmay be captured and used as an energy source, such as to offset energyrequirements of the wastewater treatment plant. The temperature in theUASB reactor is typically 18° C. or higher. Further conditions of theUASB reactor include a hydraulic retention time of at least 3 to 24hours, and the sludge retention time is at least 15 days. Even further,overflow velocity is around or less than 3 feet/hour. The biochemicalprocesses in typical UASB reactors typically include hydrolysis orsolubilization, acidogenesis or acetogenesis, and tnethanogenesis. Thefirst step of hydrolysis typically takes 10-15 day for complex organicsto be solubilized so that they can be absorbed into the bacteria cellswhere they are degraded by endoenzymes. The second step of acidogenesisutilizes another group of organisms to form organic acids. The thirdstep of methanogenesis involves methane-producing anaerobic bacteria tocomplete a decomposition process.

As shown in FIG. 7, plant influent wastewater 710 is directed into aUASB reactor 712. As a result of the reactions that take place in theUASB reactor 712, biogas 714 is produced, which typically includesmethane, nitrogen, and carbon dioxide. Also from the UASB reactor 712 isa stream of sludge 718, which is directed to sludge processing 726. Insome instances, a portion 716 of the plant influent wastewater 710 isdiverted around the UASB reactor 712 to the pretreated stream 720. Thistypically occurs when the plant influent wastewater 710 includes a highamount of ammonia such that more carbon is needed in the Anox-P process722. The pretreated stream 720 then flows to the Anox-P process 722,which produces plant effluent 724.

Turning now to FIG. 8, a schematic view 800 of a wastewater treatmentprocess that utilizes chemically enhanced primary treatment (CEPT) isshown, in accordance with an embodiment of the present invention.Generally, CEPT involves chemicals, such as metal salts and/or polymers,being added prior to a primary sedimentation basin such that thechemicals cause suspended particles to clump together via coagulationand flocculation. This provides for a more thorough and fasteraggregation time for the particles such that the treatment efficiency isenhanced. Many times, no residual metals are present in the supernatant.Some of the other chemicals used in CEPT may include ferric chloride andaluminum sulfate. A CEPT tank, such as a settling tank, may be used inthe CEPT process. Advantages of CEPT to other processes include a moreaffordable and efficient option when compared to conventional types oftreatment. Typically, CEPT processes consist of bar screens, a gritchamber, solid-liquid separation step such as a settling tank, which inone embodiment is a primary clarifier. Other types of solid-liquidseparation steps can also be used, such as screening or dissolved airflotation.

As shown in FIG. 8, the plant influent wastewater 810 enters the CERT812, where sludge 814 from the CERT 812 is first directed to thickening816, then the sludge 816 is directed to anaerobic digestion 820. As aresult of anaerobic digestion 820, biogas 822 is formed, which consists,at least, of methane and carbon dioxide. Further, sludge 824 from theanaerobic digestion 820 is sent to sludge processing 826. From the CERT812, pretreated effluent 828 is sent to the Anox-P process 820, whereplant effluent 832 is generated having much reduced amounts of nitrogen,phosphorus, etc. Excess sludge 834 from the Anox-P process 830 is sentto the anaerobic digestion 820 for stabilization and additional methanegeneration.

Referring to FIG. 9, a schematic view 900 of a wastewater treatmentprocess that utilizes a one-stage activated sludge system is depicted,in accordance with an embodiment of the present invention. A two-stageactivated sludge system is typically referred to as the AB process,wherein the first stage, or “A” stage is for COD reduction using a grittank, bioreactor, and intermediate clarifier, and the second stage, or“B” stage is for nitrification and N-removal and typically includes abioreactor and a secondary clarifier. However, in the embodiment of FIG.9, only the first stage is utilized while the second stage is replacedwith the Anox-P process as described herein. The effluent is directed tothe Anox-P process for further processing. In some embodiments, up to90% of the carbon present in the influent stream may be removed by wayof the one-stage activated sludge system. The one-stage activated sludgesystem depicted in FIG. 9 may have a sludge retention time (SRT) of 0.5days. It is typically a high-rate but low SRT of less than one day, andsometimes as low as 0.5 days. The COD removal (removal of carbon) isaround 70-80%.

As shown in FIG. 9, plant influent wastewater 910 enters the one-stageactivated sludge system 912. Excess sludge 914 from this system flows tothickening 916, and then the sludge 918 flows to anaerobic digestion. Asa result of the anaerobic digestion 920, biogas 922 is formed, and mayinclude methane and carbon dioxide. The pretreated effluent 924 from theone-stage activated sludge system 912 enters the Anox-P process 916,where plant effluent is formed by the removal of nitrogen, phosphorus,etc.

FIG. 10 illustrates a schematic view 1000 of a wastewater treatmentprocess that utilizes a one-stage activated sludge system, in accordancewith an embodiment of the present invention. FIG. 10 illustrates a moredetailed view of the one-stage activated sludge system 912 of FIG. 9.The plant influent wastewater 1010 is directed to a grit tank 1012,whose effluent 1014 is sent to a bioreactor 1016. From the bioreactor1016, the effluent 1018 is sent to an intermediate clarifier 1020. Theintermediate clarifier 1020 marks the end of the one-stage activatedsludge system, such that the pretreated effluent 1028 is sent to theAnox-P process 1030 for further processing. A portion of the sludge 1022from the intermediate clarifier 1020 may be recycled to the streamentering the grit tank 1012 as return activated sludge 1026, and aportion is diverted for further treatment as excess sludge 1024.

Turning now to FIG. 11, a bar graph is shown of a comparison of energyintensity using various water treatment systems, in accordance with anembodiment of the present invention. Energy utilization is compared andshown in FIG. 11. The bar graph compares a conventional nitrificationdenitrification process (labeled “typical”), with results from anenergy-neutral wastewater treatment plant (“Strass”), and finally withanaerobic pretreatment combined with Anox-P treatment, as describedherein (“Anaerobic pretreatment+Anox P”). As shown, the energy requiredfor anaerobic pretreatment combined with the Anox-P system is reducedwhen compared with the other systems. One reason for this is that energyutilization required for aeration is about 50% of other systems, eventhough full nitrification-denitrification is still achieved, evenwithout an external carbon source. In one embodiment, sludge from thepretreatment process and waste activated sludge from the Anox-P processundergo anaerobic digestion. The biogas from the digestion process maybe utilized for on-site energy generation.

Referring to FIG. 12, a bar graph illustrates a comparison of energygeneration from biogas, in accordance with an embodiment of the presentinvention. The energy generation shown in FIG. 12, in one embodiment, isfrom anaerobic digestion of the sludge produced from various processes.FIG. 12 illustrates the energy conversion efficiency from energy in theproduced methane converted to electric energy.

Many different arrangements of the various components depicted, as wellas components not shown, are possible without departing from the scopeof the claims below. Embodiments of the technology have been describedwith the intent to be illustrative rather than restrictive. Alternativeembodiments will become apparent to readers of this disclosure. Further,alternative means of implementing the aforementioned can be completedwithout departing from the scope of the claims below. Certain featuresand subcombinations are of utility and may be employed without referenceto other features and subcombinations and are contemplated within thescope of the claims.

The invention claimed is:
 1. A process for treating wastewater tosimultaneously remove organic matter, nitrogen, and phosphorus withenergy recovery, the process comprising: providing an ammonia-containingstream in a pretreatment tank that produces, at least, excess sludge,biogas, and a pretreated stream, wherein the pretreated stream has atleast 45% less carbon than the ammonia-containing stream, and whereinthe biogas comprises at least methane and carbon dioxide; flowing thepretreated stream and return activated sludge to an anoxic tankoperating under anoxic conditions; mixing the pretreated stream and thereturn activated sludge in the anoxic tank to form a mixed liquor,thereby initiating phosphorus release and fermentation of particulateorganic matter and dissolved organic matter; transferring the mixedliquor to an aerated tank operating under microaerophilic conditions,wherein a concentration of dissolved oxygen in the aerated tank is lessthan 1.0 mg/l of the mixed liquor, which is effective to promotesimultaneous nitrification, denitrification, phosphorous release, andphosphorus uptake in the aerated tank; and transferring the mixed liquorto a membrane tank that separates treated effluent from activated sludgecontaining microorganisms, wherein a first portion of the activatedsludge is returned to the anoxic tank as the return activated sludge. 2.The process of claim 1, wherein the ammonia-containing stream is plantinfluent wastewater that is to be treated by converting the ammonia tonitrogen gas and water.
 3. The process of claim 1, wherein the biogascomprises about 60% of the methane.
 4. The process of claim 1, whereinthe pretreatment tank is an upflow anaerobic sludge blanket (UASB)reactor.
 5. The process of claim 2, wherein the biogas is treated suchthat it can be used to power a wastewater treatment plant that treatsthe plant influent wastewater by offsetting energy requirements of thewastewater treatment plant.
 6. The process of claim 1, wherein themicroaerophilic conditions in the aerated tank promote the fermentationof the particulate organic matter in the mixed liquor and allow fordevelopment of a microbial population used for phosphorus removal. 7.The process of claim 1, wherein a portion of the ammonia-containingstream bypasses the pretreatment tank and is directed to the anoxictank.
 8. The process of claim 1, wherein the pretreatment tank utilizeschemically enhanced primary treatment (CEPT).
 9. The process of claim 1,wherein the pretreatment tank utilizes a one-stage activated sludgesystem.
 10. A method for reducing ammonia in a stream while recoveringenergy, the method comprising: providing a stream containing ammonia ina pretreatment tank that comprises anaerobic microorganisms that reactwith the ammonia-containing stream to produce biogas and a pretreatedstream; contacting the pretreated stream with an oxygen-containingstream in an anoxic tank under effective treatment conditions to form afirst product stream, the ratio of ammonia in the pretreated stream tooxygen in the oxygen-containing stream being about 2.28 g O₂/g N—NH₃(2.28 grams of oxygen per gram of nitrogen in ammonia) or less; andexposing the first product stream to organic matter in an aerated tankunder effective treatment conditions in a ratio of about 0.57 g COD/gN—NH₃ (0.57 grams of chemical oxygen demand (COD) per gram of nitrogenin ammonia) or less.
 11. The process of claim 10, wherein the biogascomprises at least 45% of the carbon present in the ammonia-containingstream.
 12. The process of claim 10, wherein phosphorus release occursin the anoxic tank.
 13. The process of claim 10, wherein nitrification,denitrification, phosphorus release, and phosphorus uptake occursimultaneously in the aerated tank.
 14. The process of claim 10, whereina concentration of dissolved oxygen in the aerated tank is less than 1.0mg/l of fluid.
 15. A system for treating wastewater to simultaneouslyremove organic matter, nitrogen, and phosphorus with energy recovery,the system comprising: a pretreatment tank that receives plant influentwastewater and that comprises anaerobic microorganisms that reacts withthe plant influent wastewater to produce, at least, biogas comprisingmethane, excess sludge, and a pretreated stream, the pretreated streamhaving at least 45% less carbon than the plant influent wastewater; ananoxic tank that receives the pretreated stream and return activatedsludge, wherein the anoxic tank operates under anoxic conditions topromote denitrification, phosphorus release and fermentation ofparticulate organic matter and dissolved organic matter; an aerated tankthat receives a mixed liquor from the anoxic tank, wherein aconcentration of dissolved oxygen in the aerated tank is less than 1.0mg/l to effectively promote development of phosphorus-release bacteriathat is present in the return activated sludge received into the anoxictank, and wherein the phosphorus-release bacteria in the returnactivated sludge allows for the phosphorus release and fermentation ofparticulate organic matter in the anoxic tank; and a membrane tank thatseparates plant effluent wastewater from activated sludge, a portion ofwhich is recycled to the anoxic tank as the return activated sludge. 16.The system of claim 15, wherein the aerated tank comprises one or moreaerated tanks.
 17. The system of claim 15, wherein the aerated tankoperates under microaerophilic conditions.
 18. The system of claim 17,wherein nitrification, denitrification, phosphorus release, andphosphorus uptake occur simultaneously in the aerated tank.
 19. Thesystem of claim 15, wherein the concentration of dissolved oxygen in thesecond tank is less than 0.3 mg/l of the mixed liquor.